EP0253563B1 - Procédé pour éliminer la vapeur de mercure et/ou la vapeur de composés organiques nuisibles et/ou les oxydes d'azote des gaz de rejet d'une installation d'incinération - Google Patents

Procédé pour éliminer la vapeur de mercure et/ou la vapeur de composés organiques nuisibles et/ou les oxydes d'azote des gaz de rejet d'une installation d'incinération Download PDF

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Publication number
EP0253563B1
EP0253563B1 EP87306035A EP87306035A EP0253563B1 EP 0253563 B1 EP0253563 B1 EP 0253563B1 EP 87306035 A EP87306035 A EP 87306035A EP 87306035 A EP87306035 A EP 87306035A EP 0253563 B1 EP0253563 B1 EP 0253563B1
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EP
European Patent Office
Prior art keywords
flue gas
spray absorption
process according
activated carbon
powdery
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
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EP87306035A
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German (de)
English (en)
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EP0253563A1 (fr
EP0253563B2 (fr
Inventor
Jens Thousig Moller
Niels Jacobsen
Kirsten Kragh Nielsen
Stig Rasmussen
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GEA Process Engineering AS
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Niro AS
Niro Atomizer AS
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Application filed by Niro AS, Niro Atomizer AS filed Critical Niro AS
Priority to AT87306035T priority Critical patent/ATE49714T1/de
Publication of EP0253563A1 publication Critical patent/EP0253563A1/fr
Publication of EP0253563B1 publication Critical patent/EP0253563B1/fr
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B01D53/70—Organic halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons

Definitions

  • mercury vapor which in this context means vapor of elementary mercury as well as mercury-containing chemical compounds in vapor phase
  • concentrations will be in the range of 100-1 000 14N m 3 .
  • chlorodibenzo-dioxins and -furans are represented by the formulae resp., wherein n and m each independently is an integer from 0 through 4 provided that n + m is at least 2.
  • the concentration of these compounds in incinerator flue gases varies considerably, dependent primarily on the temperature prevailing in the combustion zone of the incinerator and on the composition of the refuse which is incinerated. Typically the concentration is 0.1-1.0 iLg/N m 3 but substantial variations also outside this range are usual.
  • Incinerator flue gases also contain considerable amounts of nitrogen oxides which are not always removed efficiently by the conventional flue gas purification steps using basic absorbants.
  • a process for removing mercury vapor from a hot hydrogen chloride-containing flue gas is disclosed in EP-A-0 013 567 (Svenska Flaktfabriken).
  • the gas which contains hydrogen chloride and minor amounts of mercury vapor is contacted with powdered calcium hydroxide, preferably in a fluidized bed.
  • the hydrogen chloride in the gas reacts with the calcium hydroxide to form calcium chloride which apparently is essential to the removal of mercury.
  • said process does not always enable reduction of mercury vapor to the required low levels, and it is without any substantial effect as to removal of the noxious organic material.
  • US-A-4,273,747 discloses removal of mercury from hot waste gases by atomizing an aqueous liquid into the waste gases in the presence of fly ash suspended in the gas and subsequently separating the fly ash together with a substantial part of the mercury originally present as vapor. It is essential that by said treatment the gas stream is cooled from a temperature of at least 200 °C to a temperature below 160 °C.
  • the aqueous liquid may be just water or it may be an aqueous solution or suspension of an alkaline compound, preferably calcium hydroxide.
  • active charcoal or coke is used to remove noxious flue gas components including heavy metals.
  • active coal or coke is used in a fixed bed which means that it should be in the form of rather coarse non-dusting particles or granulates which are expensive to produce and are less active than a corresponding powdery adsorbent.
  • US-A-4,061,476 discloses a gas purification method in which a pulverulent solid sorption agent is injected into a stream of noxious-contaminant-containing gas subjected to intensive turbulence and subsequently separated from the gas.
  • a pulverulent solid sorption agent is injected into a stream of noxious-contaminant-containing gas subjected to intensive turbulence and subsequently separated from the gas.
  • powdery filtering charcoal is suggested without indication of the contaminations for which this specific sorption agent is intended.
  • the absorbents are advantageously of grain sizes of less than 100 ⁇ m, preferably less than 50 pm.
  • the sorption agent is activated carbon in the form of fine particles efficient separation of the carbon from the gas stream cause troubles. This applies both when electrostatic precipitators and fabric filters are used for the separation.
  • the present process uses the activated carbon as a fine powder which is suspended in the gas stream and subsequently removed therefrom together with the particulate material formed by the spray absorption process.
  • pulverized activated carbon involves certain advantages over the use of a coarse or granulated carbon due to the relatively higher adsorption capacity of the powdery material and the lower price thereof.
  • Fine carbon particles are not easily removed by means of a mechanical filter such as a baghouse, since the fine carbon particles tend to block the filter and thereby create an unacceptably high pressure drop over the filter.
  • electrostatic precipitators are less efficient than desired to remove fine particles of activated carbon occurring as sole particulate material in a gas stream. This is due to the fact that the carbon particles have a too low electric resistivity (or a too high conductivity) which means that they loose their electric charge when contacting the ground electrode of the electrostatic precipitator. Thereby the carbon particles are not efficiently retained but tend to become resuspended in the gas stream. This results in an unsatisfactory particle separation from the gas stream unless the consumption of electric energy is increased substantially.
  • the presence of the particulate material formed by the spray absorption facilitates the recovery of the powdery activated carbon from the gas stream, not only when a baghouse is used as particle separator but also when particle separation is performed by means of an electrostatic precipitator.
  • the particulate material formed in the spray absorption process together with any fly ash present and the flue gas acts as filter aid thereby permitting building up of a powder layer having a substantial thickness on the filter surfaces without undue increase of the resistance to gas passage and consequently without a large pressure drop over the filter.
  • the fine particles of activated carbon are embedded in the powder layer thus deposited on the filter surface and dust problems due to penetration of the carbon particles through the filter are avoided and increase of pressure drop over the filter is substantially delayed.
  • the particulate material formed in the spray absorption process also has the effect of facilitating the removal of the carbon particles because said particulate material by covering the electrode forms a layer into which the small carbon particles are bound and which layer impedes direct contact between the particles and the electrodes whereby undue discharge of the carbon particles is avoided.
  • resuspension of the carbon particles in the stream of gas is less likely to take place and the carbon particles are recovered from the electrostatic precipitator in admixture with said particulate material and any fly ash originally present in the flue gas.
  • the term « powdery activated carbon is used in a somewhat broader sense than said term is usually applied in commerce.
  • said term is not limited to cover materials which have been subjected to an « activation » treatment, e. g. with vapor.
  • the term is intented to cover also powdery carbonacious materials such as coal, coke or the like which have an adsorption activity which is not the result of a special activation but which is inherent in the powdery material already when formed, e. g. by grinding or by thermal decomposition.
  • the absorption material used in the present process may be substantially cheaper than commercial activated carbon which has usually been subjected to special activation and purification procedures.
  • powdery is used to distinguish the carbonacious material used in this process from the granulated activated carbons conventionally used as fixed bed adsorbents for gas purification.
  • the very high adsorption efficiency of the activated carbon in the process according to the invention is a result of the improved adsorption conditions provided by the cooling of the gas stream which takes place in the spray absorption process performed immediately after, during or immediately before the introduction of the powdery activated carbon into the gas stream.
  • the powdery activated carbon When the powdery activated carbon is injected into the flue gas stream at a location downstream of the spray absorption chamber it is preferred to use a baghouse as particle separator because an intimate contact between flue gas and carbon is obtained when the flue gas passes through the carbon containing layer of particulate reaction products which builds up on the filter surfaces.
  • the present process is also suitable for being performed using a plant in which particles are separated by means of an electrostatic precipitator. Since contact between flue gas and collected particulate material is less intimate in an electrostatic precipitator than in a baghouse filter it is preferred to inject the powdery activated carbon into the gas stream at a location at some distance from the electrostatic precipitator, e. g. in the spray absorption chamber or upstream of said chamber.
  • the basic absorbent atomized in an aqueous suspension or solution into the spray absorption chamber is preferably calcium hydroxide (hydrated lime, slaked lime), sodium carbonate or hydrogen carbonate or pulverized limestone.
  • fly ash from incinerator plants has a certain ability to remove mercury vapor from flue gas when present in the hot flue gas during the cooling thereof by atomizing aqueous liquids into the hot flue gas.
  • any fly ash present in the flue gas to be cleaned and only separate it from the gas together with the particulate material comprising reaction products of the basic absorbent with acidic components of the flue gas, non-reacted basic absorbent and activated carbon.
  • the process according to the invention may also be successfully performed on flue gas from which the fly ash has been removed in a preceding particle separation step.
  • nitrogen oxides are usually present in incinerator flue gases in amounts several orders of magnitude higher than the amounts of mercury and POM, it is preferred to use relatively large quantities of carbon, e. g. 100-500 mg/N m 3 , when an efficient removal of nitrogen oxides is aimed at.
  • a duct 1 which carries a stream of hot incinerator waste gas which besides acidic components such as HCI, S0 2 and nitrogen oxides contains mercury vapor and noxious organic matter, especially chlorodibenzodioxin and -furans.
  • the waste gas also contains fly ash.
  • duct 1 debouches a pipe 2 connected to a pneumatic system 3 for providing a constant amount of powdery activated carbon to the flue gas.
  • the system 3 comprises a hopper 4 for powdery activated carbon and a screw feeder 5 adjusted to deliver a constant rate of carbon or controlled to provide carbon in dependency on the amount and composition of the flue gas stream in duct 1.
  • the system 3 is provided with pressurized air through conduit 6.
  • the carbon may, of course, be injected by any other means suitable for dispersing into the flue gas.
  • the carbon powder is entrained by the waste gas in duct 1 and carried to a spray absorption chamber 7.
  • an aqueous absorbent such as a suspension of lime of linestone or a solution of sodium carbonate or sodium hydrogen carbonate, provided through duct 8, is atomized to small droplets.
  • the water evaporates from the atomized droplets whereby the temperature of the gas decreases substantially and at the same time acidic substances in the waste gas react with the basic absorbent producting a particulate material primarily comprising salts formed by said reaction, together with non-reacted absorbent.
  • the pipe 2 may debouch in the very spray absorption chamber 7 (as indicated by the dotted lines).
  • a particulate material comprising said reaction products, non-reacted absorbent, possible fly ash and activated carbon may be recovered from the bottom of the spray absorption chamber through 9 whereas the remaining part of said reaction products and non-reacted absorbent and nearly all the activated carbon and fly ash remain suspended in the gas until the gas reaches an electrostatic precipitator 10, in which substantially all particulate material is separated and removed through 11.
  • the gas from which a substantial part of mercury vapor and noxious organic matter, especially chlorodibenzo-dioxin and-furans, originally present therein, have been absorped, may be discharged to the atmosphere via a stack 12.
  • the system 3 for providing powdery activated carbon injects the carbon at a location downstream of the spray absorption chamber 7.
  • the particle collector is a baghouse 13 from where the powdery carbon mixed with particulate material formed in the spray absorption chamber 7 and mixed with any fly ash originally present in the flue gas in duct 1, is recovered through conduit 14.
  • This example was performed in a pilot plant of the type depicted in fig. 2 treating 300 N m 3 /h flue gas.
  • the temperature of the flue gas supplied through duct 1 varied from 230 °C to 300 °C.
  • An aqueous suspension of slaked line was atomized in the spray absorption chamber 7 to obtain a total removal of 80-95 % of acidic components (HCI and 50 2 ) in the process.
  • the baghouse 13 was of the pulse jet type.
  • Powdery activated carbon was injected between the spray drying absorption chamber and the pulse jet filter in amounts as indicated in table 1 below.
  • the powdery activated carbon was of a quality which has a total surface area (determined by the BET method) of 1 000-1 100.m?/g, a pore volume of 0.8-0.95 cm 3 /g and a mesh size corresponding to a screen analysis (passing 44 ⁇ m apertures) of 65-85 %. Microscopic examination indicates that most particles have a diameter of 1 ⁇ m or less.
  • the material is produced by pulverizing bituminous coal and is activated by steam treatment.
  • the incinerator gas stream used in all four tests had a fly ash content of approximately 2 g/Nm 3.
  • the tests were made on an industrial plant receiving 100,000 Nm 3 /hour incinerator flue gas having an approximate temperature of 240-260 °C and a fly ash content of approximately 2,5 g/Nm 3 .
  • This example illustrates that also when particle separation takes place by means of an electrostatic precipitator it is possible to achieve an efficient removal of mercury by the present process.
  • Incinerator flue gas was applied through duct 1 in an amount of 300 Nm 3 /h.
  • the fly ash content of said flue gas was 2 g/Nm 3 and the temperature varied between 203-300 °C.
  • the baghouse 13 was of the pulse jet type.
  • the temperature of the flue gas before treatment was 240-280 °C.
  • This example demonstrates the ability of the present process for reducing the amount of nitrogen oxides in the flue gas from incinerator plants.
  • the incinerator flue gas was supplied in an amount of approximately 60,000-100,000 Nm 3 /h at a temperature of approx. 240-280 °C.

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  • Chemical & Material Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)
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  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Claims (10)

1. Procédé pour éliminer la vapeur de mercure et/ou la vapeur de composés organiques nuisibles et/ou les oxydes d'azote d'un courant de gaz chauds de rejet d'une installation d'incinération, lesdits gaz de rejet pouvant éventuellement contenir des cendres volantes, avec élimination simultanée de composants acides desdits gaz de rejet par passage du courant, à une température de 135 à 400 °C, dans une chambre d'absorption par pulvérisation, dans laquelle une suspension aqueuse d'un agent absorbant basique est pulvérisée pour refroidir les gaz de rejet à une température de 180 à 90 °C pour absorption des composants acides des gaz de rejet et pour évaporation simultanée de l'eau de ladite suspension, avec formation d'un matériau en particules contenant des produits de réaction entre l'absorbant basique et les composants acides des gaz de rejet ainsi que de l'absorbant qui n'a pas réagi, ledit matériau en particules et les cendres volantes éventuelles étant séparés des gaz rejet dans un séparateur de particules en aval de la chambre d'absorption par pulvérisation, procédé dans lequel on injecte du charbon actif pulvérulent en quantité de 1 à 800 mg par Nm3 de gaz de rejet dans le courant de gaz de rejet en au moins un endroit choisi parmi des emplacements en amont de la chambre d'absorption par pulvérisation, des emplacements dans la chambre d'absorption par pulvérisation et des emplacements en aval de la chambre d'absorption par pulvérisation, mais en amont du séparateur de particules, et on sépare ledit charbon pulvérulent dans le séparateur de particules avec ledit matériau en particules.
2. Procédé selon la revendication 1, dans lequel le charbon pulvérulent est injecté dans le courant de gaz de rejet en un emplacement situé en aval de la chambre d'absorption par pulvérisation.
3. Procédé selon la revendication 1 ou la revendication 2, dans lequel ledit matériau en particules et le charbon pulvérulent ainsi que les cendres volantes éventuelles sont séparés du gaz de rejet à l'aide d'un sac filtrant.
4. Procédé selon la revendication 1, dans lequel le charbon pulvérulent est injecté dans le courant de gaz de rejet en un endroit choisi parmi des emplacements en amont de la chambre d'absorption par pulvérisation et des emplacements dans ladite chambre.
5. Procédé selon la revendication 1 ou la revendication 4, dans lequel ledit matériau en particules et le charbon pulvérulent ainsi que les cendres volantes éventuelles sont séparés du gaz à l'aide d'un précipitateur électrostatique.
6. Procédé selon la revendication 1, dans lequel l'agent absorbant basique est choisi parmi de l'hydroxyde de calcium, des carbonates de sodium et de la pierre calcaire.
7. Procédé selon la revendication 1, dans lequel on utilise un charbon actif pulvérulent dont la taille de particule en permet le passage d'au moins 40 % en poids à travers un tamis à mailles de 40 µm par tamisage humide, et qui sous examen au microscope présente une taille moyenne de quelques µm, ou moins.
8. Procédé selon la revendication 1, en particulier pour l'élimination de vapeur de mercure et/ou de vapeur de composés organiques nocifs, et dans lequel le charbon pulvérulent est injecté dans les gaz de rejet, en une quantité de 5 à 100 mg par Nm3.
9. Procédé selon la revendication 1, dans lequel le gaz est refroidi à une température de 100 à 150 °C au cours de l'étape d'absorption par pulvérisation.
10. Procédé selon la revendication 1, en particulier pour l'élimination d'oxydes d'azote, et dans lequel le charbon pulvérulent est injecté dans le gaz de rejet, en une quantité de 100 à 500 mg par Nm3.
EP87306035A 1986-07-16 1987-07-08 Procédé pour éliminer la vapeur de mercure et/ou la vapeur de composés organiques nuisibles et/ou les oxydes d'azote des gaz de rejet d'une installation d'incinération Expired - Lifetime EP0253563B2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87306035T ATE49714T1 (de) 1986-07-16 1987-07-08 Verfahren zur entfernung von quecksilberdampf und/oder daempfen schaedlicher organischer verbindungen und/oder stickstoffoxiden aus rauchgas von einer verbrennungsanlage.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DK3381/86 1986-07-16
DK338186A DK158376C (da) 1986-07-16 1986-07-16 Fremgangsmaade til nedbringelse af indholdet af kviksoelvdamp og/eller dampe af skadelige organiske forbindelser og/eller nitrogenoxider i roeggas fra forbraendingsanlaeg

Publications (3)

Publication Number Publication Date
EP0253563A1 EP0253563A1 (fr) 1988-01-20
EP0253563B1 true EP0253563B1 (fr) 1990-01-24
EP0253563B2 EP0253563B2 (fr) 1996-04-17

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EP87306035A Expired - Lifetime EP0253563B2 (fr) 1986-07-16 1987-07-08 Procédé pour éliminer la vapeur de mercure et/ou la vapeur de composés organiques nuisibles et/ou les oxydes d'azote des gaz de rejet d'une installation d'incinération

Country Status (9)

Country Link
US (1) US4889698B1 (fr)
EP (1) EP0253563B2 (fr)
JP (1) JPH0829219B2 (fr)
AT (1) ATE49714T1 (fr)
CA (1) CA1300347C (fr)
DE (1) DE3761471D1 (fr)
DK (1) DK158376C (fr)
HK (1) HK54691A (fr)
NO (1) NO168510C (fr)

Cited By (3)

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DE4233303C1 (de) * 1992-10-03 1994-01-20 Metallgesellschaft Ag Verfahren zur Abtrennung von Dioxinen und Furanen aus Abgasen von Verbrennungsanlagen
US6843835B2 (en) 2001-03-27 2005-01-18 The Procter & Gamble Company Air cleaning apparatus and method for cleaning air
CN1798599B (zh) * 2003-06-03 2010-05-05 阿尔斯托姆科技有限公司 固体燃料燃烧的烟道气的脱汞方法和装置

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JPS6369524A (ja) * 1986-09-12 1988-03-29 Gadelius Kk 多塩化ジベンゾパラジオキシン除去装置
EP0343672A1 (fr) * 1988-05-26 1989-11-29 Jednotne Zemedelske Druzstvo Podhaji Méthode et dispositif pour purifier des mélanges de gaz d'hydrocarbures lourds et de leurs dérivés
SE465111B (sv) * 1989-04-07 1991-07-29 Flaekt Ab Foerfarande vid rening av vid foerbraenning av avfall bildad roekgas
DE3919124A1 (de) * 1989-06-12 1990-01-18 Haji Javad Mehdi Dr Ing Verfahren zur abscheidung von polyzylkischen kohlenwasserstoffen und schwermetallen aus abgasen
DE3921578A1 (de) * 1989-06-30 1991-01-03 Rheinische Braunkohlenw Ag Verfahren zur reinigung von rauchgas aus verbrennungsanlagen
DE4012982A1 (de) * 1990-04-24 1991-10-31 Ftu Gmbh Verfahren zur reinigung von gasen und abgasen von anorganischen und organischen schadstoffen
EP0454885A1 (fr) * 1990-05-02 1991-11-06 Ftu Gmbh Procédé pour la purification de gaz et de gaz d'échappement de polluant
DE4034498A1 (de) * 1990-09-06 1992-03-12 Metallgesellschaft Ag Verfahren zur abtrennung von schwermetallen und dioxinen aus verbrennungsabgasen
US5260047A (en) * 1990-10-05 1993-11-09 Linde Aktiengesellschaft Process for purifying waste gases containing polyhalogenated compounds
CH689375A5 (de) * 1991-04-17 1999-03-31 Von Roll Umwelttechnik Ag Verfahren zum Reinigen von Rauchgasen.
US5238665A (en) * 1991-06-10 1993-08-24 Beco Engineering Company Method for minimizing environmental release of toxic compounds in the incineration of wastes
DE4124844A1 (de) * 1991-07-26 1993-01-28 Krc Umwelttechnik Gmbh Verfahren zur reinigung von stark mit quecksilber belasteten rauchgasen
DE4127075A1 (de) * 1991-08-16 1993-02-18 Nymic Anstalt Verfahren zum reinigen von belasteten abgasen von verbrennungsanlagen
JPH0564718A (ja) * 1991-09-05 1993-03-19 Daikin Ind Ltd 濃縮方法および装置
US5435980A (en) * 1991-11-04 1995-07-25 Niro A/S Method of improving the Hg-removing capability of a flue gas cleaning process
DE4303450C2 (de) 1993-02-05 1997-07-03 Rheinische Kalksteinwerke Mittel zur trockenen Reinigung von Abgasen
CA2114331C (fr) * 1993-06-10 2000-03-28 Bernard J. Lerner Elimination du mercure, du cadmium et de leurs composes presents dans les gaz de combustion
CA2130317C (fr) * 1993-10-01 2000-01-18 Bernard J. Lerner Formation de dioxine dans des gaz de combustion de carneau
DE4344113A1 (de) * 1993-12-23 1995-06-29 Metallgesellschaft Ag Verfahren zur Reinigung von Abgasen der Abfallverbrennung
DE4404284A1 (de) * 1994-02-11 1995-08-17 Steag Ag Anordnung und Verfahren zur umweltverträglichen Rauchgasreinigung
US5505766A (en) * 1994-07-12 1996-04-09 Electric Power Research, Inc. Method for removing pollutants from a combustor flue gas and system for same
US5507238A (en) * 1994-09-23 1996-04-16 Knowles; Bruce M. Reduction of air toxics in coal combustion gas system and method
JPH08182918A (ja) * 1994-12-28 1996-07-16 Kawasaki Heavy Ind Ltd 微粉炭素による流動層脱硝方法及び装置
US5672323A (en) * 1995-01-26 1997-09-30 The Babcock & Wilcox Company Activated carbon flue gas desulfurization systems for mercury removal
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NO872927D0 (no) 1987-07-14
US4889698B1 (en) 2000-02-01
DK338186A (da) 1988-01-17
EP0253563A1 (fr) 1988-01-20
CA1300347C (fr) 1992-05-12
NO168510B (no) 1991-11-25
DK158376B (da) 1990-05-14
ATE49714T1 (de) 1990-02-15
US4889698A (en) 1989-12-26
EP0253563B2 (fr) 1996-04-17
HK54691A (en) 1991-07-26
JPH0829219B2 (ja) 1996-03-27
DK158376C (da) 1990-10-08

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